Apparatus for converting petroleum and like oils



Jam 2, 1940- T. P. SIMPSON Er A1. 2,185,931

APPARATUS FOR CONVERTING PETROLEUM AND LIKE OILS Filed Sept. 1, 1937 4 Sheets-Sheet l 72. Z7 mw Jan. 2, 1940.

* T. P. SIMPSON ET Al. 2,185,931

APPARATUS FOR CONVERTING PETROLEUM AND LIKE OILS Filed sept. `1, 1957 4 sheets-sheet 2 ya 5% www Jan. 2, 1940. T. P. SIMPSON ET A1.

'APPARATUS FOR GONVERTING PETROLEUM AND LIKE oILs Filed sept. 1, 1957 4 Sheets-Sheet 3 M, Y s i W wWWwyw fama@ p/C/ 5. E 0,0 Ln @www/L v #of n Jan. 2, 1940, T, P. sxMPsoN ET AL 2,185,931

APPARATUS FOR CONVERTING PETROLEUM AND LIKE OILS Filed Sept. l, 1937 4 Sheets-Sheet 4 9 q, ono

u Dango i dump Patented Jan. 2, 1940 APPARATUS FOR CONVERTING PETROLEUM AND LIKE OILS Thomas P. Simpson, John W. Payne, and John A.

Crowley, Jr., Woodbury, and Clark S. Teltsworth, Plainfield, N. J., assignors to Socony- Vacuum Oil Company, Incorporated, New York, -N. Y., a corporation of New York Application September 1, 1937, Serial No. 162,071

6 Claims.

This invention relates particularly to apparatus for conducting catalytic reactions upon hydrocarbon oils, and in general has to do with apparatus suitable for subjecting petroleum products to reactions which are conducted in the presence of a contact mass, including regeneration of the contact mass. The present invention is directed to an apparatus of the general type disclosed and claimed in our co-pending application Serial No. 162,068, filed September l, 1937, which apparatus was devised to afford means for carrying out catalytic processes in general, such as disclosed and claimed in our co-pending application Serial No. 162,069 filed September 1, 1937. The apparatus herein disclosed and claimed was devised to aord means particularly adapted for carrying out processes of catalytic conversion of hydrocarbon oils as, for instance, such as disclosed in our co-pending case Serial No. 162,070, filed September 1, 1937. Our co-pending applications, Serial Nos. 162,540-` 162,541 and 162,542, led September 4, 1937 are likewise directed to processes and apparatus for catalytic conversion of the same general type as that of Serial Nos. 162,068 and 162,069. However, among other features the three former cases are directed to novel features of reversal of fluid flow, continuous flow of catalytic material and temperature controlling of catalytic material respectively.

' Many types of conversions of hydrocarbons into materials of different properties, physical and/or chemical, are carried on by contacting the hydrocarbons, frequently in vapor form and at high temperature, with a contact mass composed of particles which themselves have a catalytic effect. or' which are impregnated with or act as a support for material of a catalytic nature appropriate to the result desired. Such operations may contemplate, for example, the conversion of hydrocarbons of high boiling point into hydrocarbons of lower boiling point by catalytic cracking in the vapor phase. Another common operation is the polymerization, under catalytic conditions. of light or gaseous hydrocarbons to form hydrocarbons of higher boiling point. Other operations of this same general nature are catalytic dehydrogenation. desulphurizing. partial oxidation or similar conversions of hydrocarbons under similar conditions. Some operations carried out Wholly or -partially in liquid phase present similar problems. The method of operation herein disclosed is applicable to such conversions in general. This invention is equally applicable to both exothermic and endothermic reactions. Of these operations, the vapor phase cracking of hydrocarbons to produce gasoline is typical, and this specication will hereinafter discuss such operation as exemplary without, however, intending to be limited thereby or thereto except by such limitations as are stated in the claims.

It is known that hydrocarbon oils of high boiling point, when properly contacted in vapor phase with a catalytic material of proper kind are converted into oils of lower boiling point of highly useful nature. Processes based upon this principle have been developed. yOne typeof catalyst which has been used is composed of granular particles of the nature of clay, which may or may not have deposited thereon or therein other materials of a catalytic nature. Mineral oil fractions of thelnature of gas oil may, for example, be conducted at temperature of say 810 F. or higher over a catalytic mass composed of cylindrical particles of catalytic (activated) clay about 21/2 mm. diameter by 4 mm. length, resulting in substantial conversion into gasoline. In most prior proposed petroleum ,catalytic converters, petroleum vapors are merely passed into a body of catalyst of large or small depth and are caused to flow through the catalyst in more or less broadcast manner. In such operations considerable diilculties are had with channeling, short circuiting, and the like, whereby some portions of the catalyst volume are never reached .by a proper amount of reaction mixture and others are consistently reached by too much reaction mixture, resulting in erratic and improper treatment. Also, localized reactions cause localized deposits of reaction products, and during regeneration of the catalyst, cause localized regeneration, which is unsatisfactory. .It has been proposed to place catalytic material in furnace tubes through which oil is passed but this is not suitable for reactions where thermal cracking is not desired, as well as for other, reasons. It has also been proposed to distil oil and then pass vapors from the distillation operation through catalyst-containing tubes submerged in the body of oil undergoing distillation. This operation is not useful, having many objections, including limitations of temperature and heat control, lack of independence between conditions outside the tubes and inside the tubes, cumbersomeness of equipment and operation.

It is an object of this invention to provide apparatus for catalytic vapor phase conversion of hydrocarbons, and in general apparatus for conducting reactions upon petroleum in the presence of a contact mass, including regeneration of said mass, which is effective in producing the desired results, avoids the various objections stated above, combines high rates of charge with high yields of desirable product, is capable of eicient and uniform use of all portions of the catalyst mass, is capable of effecting rapid, complete, uniform, and readily controlled regeneration of catalyst in situ, is economical in operation aswell as simple and exible, and is characterized by economical design, construction, and maintenance.

transverse to the direction of ow of reaction material if the rate of reaction in the various portions of that path be properly controlled, and that the necessary control may be accomplished by properlfy Y forming the catalyst paths and placing adjacent them paths for heat exchange medium, establishing the proper relation between such paths and the contents thereof, and continuously and positively circulating a heat transfer medium in proper heat exchange rela.- tionship with the catalyst. The reaction method practised in the apparatus of this invention leaves the spent catalyst in a condition well fitted for easy and uniform regeneration, and with the regeneration also conducted in the apparatus of the invention, a. unitary conversion system of great utility results therefrom.

Effective control of conditions throughout the catalyst or contact mass is an important element of the invention. This invention provides apparatus for conducting the reactions referred to herein, including regeneration of contact material in. situ, by means of which such effective control of conditions is accomplished, thereby attaining correspondingly effective operation. Proper flowof reactants through the contact mass is effected, so that all portions of the fluid traversing the mass receive substantially identical treatment, thus promoting uniformity of reaction and uniformity of quality in the reaction product. This is accomplished by providing a plurality of long unit paths of flow, having at least one relatively short cross-dimension, through the contact mass, wherein the variation in 4length of paths travelled by dierent portions of the fluid flowing through the mass is small. In one embodiment, provision may be made for by-passing virtually any desiredsection of each unit path so that, in case the path becomes blocked at some point, as for instance by accumulated fines, unburned carbon, or the like, instead of the entire path becoming useless or impaired, the particular point inthe path which is blocked is ,by-passed and substantially full use of the contact mass throughout the remainder of the path is secured. Various embodiments accomplishing this are illustrated in the drawings and described herein. This subject matter as well as the broad concept -disclosed in this and our other applications noted above is claimed in our copending application Serial No. 308,058, filed December '7, 1939.

Effective temperature control throughout the contact mass is accomplished. Heat transfer elements are associated with the respective catalyst paths, and every part of the contact mass lies sufliciently close to a heat transfer element to insure notable uniformity of temperature throughout the entire contact mass. Heat can be put into the contact mass or removed from it as desired. Heat distribution between different portions of the catalyst mass is effected. This means for effecting this transfer of heat and control of temperature preferably involves positive circulation -at relatively high velocity of heat transfer medium through the heat transfer elements. A high boilingpoint liquidhaving a relatively high unit volume heat. absorption capacity per degree temperature lchange is preferred, although uid media such as vapors, steam, gas, air, or the like,

may be used. Means for heating or cooling the circulating heat transfer medium are provided.

A small volume of heat transfer medium relative to volume .of contact mass is used. This conserves size and cost of apparatus, with a high proportion of total apparatus volume occupied by contact mass.` It gives flexibility to the operation of the apparatus, because the entire volume of heat transfer medium in the apparatus is renewed at short intervals by the recirculation, with corresponding quick response of the apparatus to the temperature control effected by adding heat to or abstracting heat from the recirculating body of heat transfer medium. This is important in practically all operations and particularly in operations where reactions are conducted in sequence at different temperature levels, Where temperature must be built up to initiate a reaction, and the like. A large area of heat transfer surface in contact with the catalyst mass relative to volume of heat transfer medium in the apparatus is used. This is important in making possible the use of a small volume of heat exchange medium with its attendant flexibility of operation just mentioned. These features result in advantages in design, construction, and cost of apparatus; e. g., fewer heat transfer fluid passages are required, wider spacing of these elements is possible, stronger headers are made possible thereby, or thinner but equally strong headers. rA high ratio of heat transfer surface to volume of contact mass is used, this being irnportant in effecting adequate temperature control throughout the entire contact mass. When such extra surface is used, this eXtra surface is utilized also to define the flow paths through the contact mass.

The foregoing novel features are important in practical operation. The optimum and limiting values of the ratios; etc., mentioned above are important to the invention and have now been reasonably well determined and are set forth in detail below. The above-described requirements for best operation have been verifled by actual trial and experimentation. Adherence to the novel principles and limits set forth herein results in advantages of extreme importance and, conversely, departure therefrom may result in serious disadvantages. For example, in the catalytic cracking of gas oil from petroleum to make gasoline, with regeneration of the catalyst in situ by burning off the deposited carbon, the operation ordinarily can be conducted with two catalyst cases built in accordance 'with the principles and data given above, one case being in regeneration while the other is on stream. Substantial departure from the principles stated herein, for example departure from the stated ratios, results in slowing down regeneration and increasing length of cycle to the point where regeneration cannot be effected during the useful on-stream time of one catalyst case, thereb'y requiring three cases instead of two. Furthermore, such departure from the requirements of this invention results in wider temperature variations within the bodyd of the contact mass, less uniformity of reaction and regeneration, and lower yield per unit volume of contact mass and per unit volume of material charged. If it is attempted to force the operation to offset some of these disadvantages, other serious objections are encountered including destruction of the catalyst' because of excessively intense burning at localized points.

The apparatus of this invention is illustrated in the accompanying drawings. In these drawand 6, set forth certain optional arrangements which may be used therein. Figures 1 and 8 show longitudinal sections in planes 90 apart of another form of apparatus embodying the same general characteristics. Figure 9 is a diagram explaining one feature of the invention. Figure 10 is a sketch showing a longitudinal sectionof.

a form ofapparatus embodying the same essentials and at present preferred for commercial practise of the invention. Figure 11 is a crosssection of the apparatus shown in Figure 10.

Figures 12 and 13 show an alternative general form of apparatus. Figure V14 isan illustration. of how the apparatus with whichthis invention is v concerned may be set upand operated for commercial practise of the process to be conducted therein.

Referring now to Figures 1 to 6, inclusive'. Figure 1 shows a longitudinal section in somewhat diagrammatic form of an apparatus embodying the essential features necessary for the practise of our invention. The apparatus of Figure 1 consists of a shell I3 lying between body members I4 and I5, and completed at either end by end pieces I6 and I1. Tube plate I8 is placed. between members |4 and I6, and tube plate I3 is placed between members I5 and I1. Tubes 2E extend between tube sheets I6 and I9 and are securely fastened into the respective' tube sheets by rolling,welding, or other form of fastening appropriate. Orifice plate 2| is placed between parts I3 and |4 and the tubes 20 pass through plate 2| without being affixed thereinto. Orince plate 22, similarly, is placed between mem'- bers I3 and I5, and tubes 20 similarly pass through orifice plate 22. The end member I1 is equipped with an inlet fitting 23 and end member I6 is equippediwith an outlet tting v24. Inlet member 25 communicates with the space inside of member I5 between plates I9 and 22, surrounding tubes 20. Outlet member 26 communieates with the space within member I4 between plates I8 and 2|, and around tubes 20. Orifice' plates 2| and 22 are equipped with orifices 21, distributed uniformly over that portion of their area not occupied by passages for tubes 20. Oil entering through inlet 25 will pass through the orices 21 in plate 22, longitudinally through the space within the shell I3, through the orifices 21 in plate 2 I, and-leave the system through tting 26. A heat exchange fluid may enter through 23, pass through tubes 20 and leave the .apparatus through fitting 24 without coming in physical contact with the oil. Tubes 20'being constructed of heat conductive material, the two fluids are in heat exchange relationship. The direction of flow of either uid may be changed without altering this relationship. The shell I3 serves as the container for a catalytic or contact massI preferably composed of granular particles. This contact mass .may be introduced and removed by making use of the openings normally covered by plates 28 and 29.'

The design and arrangement of the tubes 20 within the shell I3 is such that thesetubes 2li also serve to divide the catalyst bed maintained in shell I3 into a large number of longitudinal passages, whose greatest length is parallel to the direction of reaction mixture flow through the shell, and which are relatively thin in at least one dimension transverse thereto. To assist in' this division, and -also to augment the ratio be- 2,185,981 ings, Figure 1 shows a longitudinal sectional view.

-no ruilt-path or passage be completely isolated .elsewhere herein should be observed. The max- 3 tween external surface and internal surface of the heatv exchange tubes 20. fins 30 are placed 'uponthe external surface of the heat exchange tubes. To properly subdivide the contact mass into 'suitable 1ongitucma1 passages, the tubes and l nns preferably should be arranged so as vto perlmit the least resistance to longitudinal flow and at the vsaine time to furnish a maximum resistance to lateralow, although it is preferred that l0 from contact with other passages for reasons stated above. The arrangement is preferably such as to give a substantially uniform crosssection area of catalyst throughout the length of each passage and of the catalyst case, which of itself promotes longitudinal iiow under uniform conditions.

Figure 2 shows a cross-section of the catalystcontaining portion of the apparatus of Figure l and sets forth a convenient and economical arrangement of tubes and fins to accomplish these purposes, which arrangement is shown in more detail in Figure 3. Figures 4, 5, and 6 showI other optional arrangements of finned tubes. In these figures the set-up is designed for the circulation of heat exchange medium inside the tubes, the contact mass being outside.

It is also possible to preserve the longitudinal positioning of. the passages within'the catalyst mass while making use of heat exchange tubes positioned transversely thereto. In Figures 'I and 8 two views 'are shown of a design in which this is accomplished. This apparatus consists of a catalyst casing 3|, mounted above a reaction mixture inlet housing 32, which is divided from the catalyst space by distributor plate 33 in which there are orifices 34. `Above the catalyst chamber is reaction mixture exit housing 35. On

Vtwo sides of the 'catalyst casing 3|, auxiliary plates 36and 31 define spaces 38 and 39, which D act as inlet and outlet chambers for heat exchange medium which may enter by 40, and leave by 4|, or the reverse, and which is conducted through the catalyst bed by a series of tubes 42 extending from side to side of the catalyst case. These tubes are arranged in vertical rows and are preferably equipped with fins 43, the tubes and ns being arranged so as to subdivide the catalyst mass into anumber of longitudinally extending paths of relatively great length in proportion to cross-section, as shown. 'I'his object mayalso be approximated by using smaller vertical spacing of unfinned tubes, while maintaining the same horizontal spacing.

As stated above, certain factors or proportions in the design of the apparatus are important features of this invention. Taking a typical example, where the catalyst mass is composed of granular particles of clay, which may themselves be the catalyst or in and/or on which an active catalytic material such as a metallic oxide is deposited, the following criteria may be used as typical of commercial design. The dimensions of the apparatus and tube spacing should be such that the unit reaction paths defined thereby should be 3 or more feet in length, up to 15 feet or more, and having at least one crossdirnension relatively short, preferably not lexceeding 1 to 2 inches. The several ratios stated imum distance of any catalyst particle from any heat extraction surface preferably should be about 1/2 inch, and not more than about 1 inch. The average. distance of any catalyst particle from a heat extraction surface is preferably about 75 A inch, and not more than about 1/2 inch. When fins are used. to insure proper heat transmission, design should be such that AT(Fin), the temperature drop from iin tip to fin base should be not greater than about 25%, and preferably about 10% of AT(Total), the temperature drop from catalyst bed to heat exchange medium. Designed proportions of fins should be such that for any cross-section of the iin, e, the length of the cross-section, divided by d, the least transverse dimension of iin (see Figure 3), should not be greater than about 12 and preferably about 4 to 8. That is, e/d=not greater than 12;

-e/d=preferably 4 to 8.

The optimum dimensions, ratios; etc., given herein are based particularly upon use of a cylindrical catalyst granule about 21/2 mm. in diameter by about 4 mm. average length, or any other shape having a like mass and percentage of void per unit volume of packed catalyst. As the catalyst particle size increases, the ratio of heat extraction surface to unit catalyst volume may decrease and the maximum distance of catalyst particle from heat extraction surface may increase. The same changes may be made with a catalyst mass of greater heat conductivity than that indicated. W'hen the design controlling operation is that of regeneration, a high degree of coking will call for increased heat extraction surface/catalyst volume ratio and decreased maximum distance, and conversely. It will be understood, therefore, that the optimum specic dimensions, ratios; etc., will vary somewhat according to the particular needs of a par- .`ticular operation. No claim is made herein to any particular composition or physical form of catalyst or contact mass.

An important feature in apparatus shown by these figures is the restricted intercommunica- -tion of one series of conduits intermediate thel r ends. For any given zone layer along the ow paths through the contact mass, which zone may be considered as being relatively thin and at substantially uniform static pressure under normal conditions of iiow, the free area for iiow between conduits in a transverse direction is relatively small compared with the free area in a direction longitudinal to the flow of reaction material. Normal flow is largely longitudinal of the respective conduits but substantial ow between cond-uits to compensate for abnormal con--- ditions is possible. Furthermore, the embodiment of these features in combination with preferred relationships defined herein constitutes an important feature of this invention.

To understand how uniform distribution of iiow may be accomplished, reference is made to Figure 9 of the drawings, in which there is shown in diagrammatic form three passages, 44, 45, and 46, each packed with contact mass and between which there is restricted communication at intervals along their length by cross passages 41.V In passage 44 there is a stoppage 48, indicated by denser packing of the contact mass.

.Equal amounts of reaction mixture, as indicated by the flow lines, are introduced at the bottom of the several paths. Only a portion,of that normally flowing in path 44 can pass through the stoppage 48. As indicated by the iiow lines, the remainder will pass through some horizontal intercommunication 41 below the stoppage, be distributed among the other paths and again through some other horizontal passage 41 above the stoppage it will return to passage 44, so that in this manner there is maintained throughout the case a. substantially uniform distribution of iiowing reaction material among the several paths and along their length by virtue of their restricted lateral intercommunication.

Figure 1D of the drawings shows a form of reaction case which not only admirably embodies the essential features of our invention, but which is perhaps more adaptable for the commercial practise of the invention than the form shown in Figure 1, in that it is able to successfully withstand the strains and distortion set up by diil'erential expansion of the several parts of the apparatus upon heating and cooling. The apparatus shown in longitudinal section in Figure 10 is enabled to handle these stresses -by means of an internal floating head arrangement. 'I'he apparat-us of Figure 10 consists of a shell 49, to which are attached end sections and 5|. vReaction mixture is admitted to the shell space 49 by inlet fitting 52 and reaction products are withdrawn by outlet fitting 53 in end member 5|. Between shell 49 and end member 50, there is placed a heavy tube sheet 54 in which are rolled tubes 55. These tubes 55 at their upper' end are secured in the tube sheet member of floating head 56. A large central tube 51 is also secured between tube sheet 54 'and the iioating head 56. Heat exchange medium is introduced by inlet fitting 51', led to the space within end fitting 50, through tubes 55 into floating head 56, thence into central tube 51 and out through outlet 58. The tubes 55 are equipped with fins 59 as before. Catalyst is confined between support plate 60 and plate 6l, both of which have orifices 62 for the passage of reaction mixture therethrough. To support plate 60 some distance above tube sheets 54 and thus provide a plenum chamber for the introduction of reaction material, there are used short lengths oi.' pipe 63 surrounding tubes 55, resting on tube sheet 54 and `supporting orifice plate 60. The iins 59 on tubes 55 extend' between plates 50 and 6|, and plate 6| conveniently may supported upon the upper ends of these fins if it be so desired. 'I'his apparatus is arranged to be installed in vertical position and may be supported conveniently by the skirt 64 as shown.

It is preferably arranged as shown for assem bly by means f bolted fianges and may be charged with catalyst before placing end piece 5| in iinai position and discharged of catalyst, at the infrequent intervals necessary, by lifting shell 49 free from tube plate 54 until the catalyst may be removed from above plate 60. It is obvious that in this design the direction of passage of either reaction material or heat exchange medium may be reversed from that indicated while preserving the essential features of operation shown. It will be seen that in this design convenient provision for the handling of differential heat expansion and the like has been made and a design convenient and economical of fabrication has been attained. Figure 11 shows a horizontal cross-section of Figure l0, taken at a point between the ends of the catalyst-containing space.

It may be seen that these various forms of apparatus all embody one general characteristic. They permit the use ofA catalyst masses which are relatively of great length in the direction of reaction material iiow and which have at least one dimension transverse thereto of relatively small magnitude, so that each portion of the catalyst therein is in effective heat exchange relationship with a positively circulated heat exchange medium by which its temperature may be controlled while in operation. Each design accomplishes this by arranging in one form or another, a series of conduits extending longitudinally of the direction of reaction material flow, which conduits are lled with a catalytic mass, and then surrounding -and/or defining these with other conduits through which ows a heat exchange medium. Each design observes certain rules of proportion of parts which are set forth herein, arid upon which the unique capability of the operation is in large part based. Provided that these rules of proportion of parts are followed, the method of operation set forth herein also may be followed in forms of construction wherein the catalyst mass is contained in tubular members properly spaced one from another, and surrounded by positively circulated heat transfer medium. Such construction is shown in Figure 12 and Figure 13.

In Figure 14, showing an operating set-up for commercial practise of this invention, 1l is a heater for charge, 12 a vapor separator, 13 and 14 are catalyst cases, 15 is a fractionator for treatment of processed vapors, 1B a condenser, and 11 a gas separator. Charge stock enters the system through pump 18, and by means of the manifold arrangement shown, any portion of it may be passed through heat exchangers 19 and 80 in any sequence desired, to be later collected in pipe 8| and passed through furnace heater 1I and into vapor separator 12, where a vaporous charge for the catalytic process, substantially free from liquid, is prepared. In case the charge stock selected is wholly vaporous at \the desired reaction temperatures, the vapor separator may be dispensed with. Any liquid separated in 12 may be removed from the system by pipe 82. Vapors from 12 pass through pipe 83, and if catalyst case 13 be on stream through pipe 84 into case 13, the valve in pipe 85 being closed. Passing through catalyst case13, the treated reaction mixture leaves through pipe 86, pipe 81 be ing closed, and through pipe 88 to fractionator 15. Material heavier than desired product is condensed in 15 and withdrawn through pipe 89 to storage, or it may be recycled in company with charge, or it may be retreated in another step of catalytic or thermal conversion. Product vapors leaving 15 through pipe 90 are condensed in 19, and separated from uncondensible gas in 11. While catalyst case 13 is on stream, catalyst case 14 will be regenerating. Regeneration medium (in this application air is used), is supplied by compressor 9 I, and passes through pipe 92 into case 14. Regeneration gases, leaving case 14 by pipe 93, may pass either through cooler 94 or through cooler 80 and after recovery of heat therefrom, are discharged to the atmosphere. Cooler 94 may be water cooled, or may be a waste heat boiler, or may heat charge for other processes, and any suitable division of flow through these two cooling means may be used. Heat transfer medium is supplied under pressure by pump 95 to discharge manifold 95, from which any desired disposal may be made to the tubes in cases 13 and 14, the heated medium, recollected in manifold 91, being passed through cooler 19 before return to the pump.

In the usual case, in the set-up shown, the heat transfer medium is 4cooled to a temperature somewhat above the reaction temperature in case 13, and a sufficient volume is passed through case 13 to supply endothermic reaction heat and at the same time insure even distribution of reaction therein. Another portion is passed through case 14, suflicient in amount to control distribution of the regeneration reaction therein, to remove excess reaction heat therefrom, and to supply kindling heat to the incoming regeneration air. Heat exchangers |09 and |01 may be used for complete individual control of the heat exchange medium going to either case 13 or 14.`

The heat transfer medium may be any suitable fluid, but is preferably a liquid such as a molten metal, a molten alloy, or fused inorganic salts, or other liquid possessed of low vapor pressure, of high heat absorbing capacity per unit volume per degree temperature change, and reasonably low viscosity at the temperature,200 to 1100- at which it is used. Preference is given to materials of low vapor pressure melting below 350 F., so that the medium may be removed from shutdown apparatus by steam heating. Convenient materials are mixtures of aluminum chloride and sodium chloride; of zinc chloride, potassium chloride and sodium chloride; or a mixture consisting essentiallyl of a mixture of sodium and potassium salts of nitrogen acids.

At the end of regeneration, air from pipe 92 is Vshut off, steam is admitted to case 14 through connection I 983 and regeneration medium and products are steamed out through regeneration gas disposal means. When case 13 comes off stream it is steamed out to the vapor system by steam admitted through connection 99. Then case 14 is put on stream and case 13 is regenerated.

As stated above, various relationships and ra-l tios involving such matters as amount of heat transferring surface, volume of heat exchange medium and volume of contact mass are important features of the invention, and have been reasonably well determined by actual operation and experimentation. The following figures represent a preferred relationship which has been found to operate satisfactorily. It will be under- Volumeof heat exchange metal (tubes and iins)=19.6 Volume occupied by molten salt in tubes 9.0

Total (volume of space occupied by catalyst, salt and heat exchange surfaces) 100.0

Heat exchange surface per cubic inch of molten salt =19.7 sq. in.

Heatexchange surface per cubic inch of metal in heat transfer tubes and iins= 9.0 sq. in. Heat exchange surface per cubic inch of molten salt pluskmetal 6.2 sq. in. Heat exchange surface per cubic inch of catalyst 2.5 sq. in.

We give the following data to define the preferred range for best design and operation:

Volume of catalyst including voids =6080% of space in catalyst zone Volume of molten salt= 2-15% of space in catalyst zone Volume of metal (tubes and fins) Volume of catalyst plus salt plus metal: 100.00% of space in catalyst zone Heat exchange surface per cubic inch of molten salt =1560 sq. in. Heat exchange surface per cubic inch of metal in heat transfer tubes and iins= 5-15 sq. in. Heat exchange surface per cubic inch -o molten salt plus metal 4-12 sq. in.

= 1.5-6 sq. in.

Heat exchange surface per cubic inch of catalys It will be understood that, while best design and operation in accordance with this invention 15-30% of space in catalyst zone set forth above, a gradual approach to such limits and ranges will naturally begin to produce some of the advantages obtained by the present invention. There is, therefore, a borderline range of relationships which do not yield the results obtainable by practise of the preferred lform of the invention but within which some of cluding voids =4090% of space in catalyst zone Volume of molten salt= 1-25% of space in catalyst zone Volume of metal (tubes 5-50% of space in catalyst zone and fins) Heat exchange surface per cubic inch of molten salt =5100 sq. in. Heat exchange surface per cubic inch of metal in heat transfer tubes and iins=330 sq. in. Heat exchange surface per cubic inch of molten salt plus metal =220 sq. in. Heat exchange surface per cubic inch of catalyst =0.5-8 sq. 1n.

These relationships and ratios, as herein set forth, define the relationship between the hydraulic radius of the catalyst path, the mass velocity of the critical reactant and the mass velocity of the heat exchange medium. The design is controlled by the ratio of heat transferred to heat liberated or absorbed in the catalyst. The heat liberated during regeneration is substantially the greatest quantity. Under proper conditions, as herein set forth, this heat lliberation may be made substantially uniform per unit volume of catalyst. Similarly, heat transfer may be made uniform per unit area of heat transfer surface. The proper proportion of catalyist volume to surface defining that volume is then shown by Heat liberated per unit time per unit volume Heat transferred per unit time per unit area wherein HR is a quantity of the nature of a hydraulic radius, having the dimension of length, and as shown hereinbefore has a broad range of from 1/8" to 2 and a preferred range of from 1/8" to The rate of heat liberation per unit .volume of catalyst is a function of the mass velocity of air (regeneration medium) in weight per unit volume of catalyst per unit of time, in proportion to coke to be burned from said catalyst, which may be applied without excessive rise in temperature sufcient to damage the catalyst. This may be expressed as a burning rate, which, while not exceeding about 1000 F. under conditions of operation, will remove coke at the rate of from about 1% by weight of catalyst to about 10% per hour for a broad range of possible operation, and from about 3% to about 6% for preferred operation. 'I'he mass velocity of heat transfer medium, of course, depends upon the specific heat and other characteristics of the medium. It is best defined as that mass velocity of heat exchange medium which will extract the required amount of heat While undergoing a tem- 'perature rise of not greater than about 50 F., and preferably of from 2 to 10 F.

Some of the advantages of the apparatus of this invention are high throughput rates per unit volume of catalyst, high conversion rates at acceptable throughputs, low coke from side and y 2,185,931 is obtained by observing the limits and ranges.

subsequent reactions, low gas from like reactions, uniformity of reaction throughout the catalyst bed, uniformity of kind of product produced from all portions of the bed, uniformity of de' posit of coke and reaction products throughout the bed, and other advantages, all of which also result indirectly in higher unit yields. As an important contribution to the flexibility and ease of control of the process, temperature oi the entire body of heat transfer medium is capable of such rapid adjustment, that dilculties due to variation in temperature level of incoming reaction mixture are practically wiped out. 'I'his is of especial time saving importance in changing over from one reaction to another, as for example, taking a case off stream in a polymerization operation at about 300 F. and putting it into regeneration at about 810 F'. Separate exchangers for heating or cooling may be installed between pump and the respective cases 'Il and 14 if desired.

The regeneration step also benefits greatly by the invention herein disclosed. The regeneration reaction is substantially uniform throughout the mass, both because the distribution of regenera-y eliminating expensive preheater installations for-- merly thought to be necessary. The regeneration heat is rejected from the system at higher temperature levels. The heat transfer medium offers an effective means whereby some of this regeneration heat may be supplied to the cracking reaction for latent heat uses.

An important feature is the ability to purge in this apparatus, between case changes, by the simple use of steam. Broadcast methods, because of their inherent tendency to by-pass and channel, cannot be steam purged eectively without extremely long and uneconomical steaming. It has being found that when using the reaction method herein disclosed, the .catalyst cases may be purged easily and completely by the simple application of steam under some pressure.

With the high charging rates possible with this invention greatly increased yields per unit of time, per unit of catalyst volume and per dollar of apparatus cost are possible. High percentage of yield on the charge can be obtained by recycling or otherwise repassing portions of the charge through the catalyst, still effecting great savings in time and cost.

These advantages flow from the use of the apparatus for conversion and the apparatus for regeneration disclosed herein,` used together as complementary parts of a unitary system of oil conversion, as carried out in the apparatus of this invention.

The catalytic reaction is preferably conducted under a gauge pressure not substantially in excess of 30 to 40 pounds per square inch. Rates of coke deposition per unit yield increase rapidly with increases in pressure, and the preferred operation is at pressures ranging from atmospheric upwards to about 20 pounds per square inch gauge. Under these conditions, it is necessary to recompress fixed gases yielded by the process in may be raised to the range 30 to 40 pounds gauge and recompression of gases avoided without sacrilice of good regeneration conditions.

The catalytic reaction for conversion of other oils to gasoline may be conducted at temperatures in the catalyst mass between about 810 F. and about 950 F. and preferably between 875 F. and 900 F. The rate of charge for such conversion will usually be in excess of twenty liters of liquid charge per hour per twenty liters of catalyst mass, and should preferably be at least fifty liters liquid charge per hour per twenty liters of catalyst. Such rates of charge and temperatures, using a charge which is clean; i. e., substantially free of unvaporized particles oi. high boiling oils and the like, prone to heavy coke formation, should result in a coke deposit amounting to from about 0.1% to about 2.0% by weight of the catalyst (average condition throughout the case) and under the preferable ranges of operation, from 0.2% to 1.5% by weight of catalyst.

The regeneration operation should be conduct` ed by the introduction of air at atmospheric temperature and under pressures very slightly above atmospheric, sufiicient only to insure flow through the apparatus at the requisite rates. The tem.- perature of regeneration should range from about 825 F. to about 1000 F. Preferred operation is at about900 F. and with a clay type catalyst,

1000 F. should not be exceeded due to possibility of rapid catalyst deterioration above those temperatures. The rate of air introduction should be such that the proper temperatures are maintained while burning oil coke at a rate oi' from about' 1% by weight of catalyst to about 10% per hour, the preferred burn-oil rate being from 3 to 6% per hour. Under these conditions the carbon dioxide in the resulting fume will range from about 3% to about 12%, the preferred range being from 6% to 11%.

It is understood that the exemplary and nuv merical data herein given are set forth largely for the purposes of illustration and that the invention is not limited therebyexcept as such limitations are expressed in the claims.

We claim:

1. An apparatus for effecting catalytic constantial length in the direction of reactant flowarranged in each of said chambers, ilns on said tubes delning passageways therebetween, catalyst material in said passageways, selective means to supply concurrently hydrocarbons to the passageways in one of said chambers` and a regenerating gas to the passageways in the other, and means for passing a temperature control medium through said closed conduits in each chamber.

2. An apparatus for effecting catalytic conversion of hydrocarbons in one zone and concurrent regeneration of catalytic .material in situ in another zone, comprising two reaction chambers, a series of closed spaced conduits of substantial length in the direction of reactant ow' arranged in each of said chambers, ns on said tubes deiining passageways therebetween, catalyst material in said passageways, selective means to supply concurrently hydrocarbons to the passageways in one of said chambers and a regenerating gas to the passageways in the other, means for passing a temperature control medium through said closed conduits in each chamber, and means to heat said temperature control medium."

3. An apparatus for eifecting catalytic conversion of hydrocarbons in one zone and concurrent regeneration of catalytic material in situ in another zone, comprising two reaction chambers, a

series of closed spaced conduits of substantial length in the direction oireactant ow arranged in each .ofsaid chambers, ns on said tubes dening passageways therebetween, catalyst material in said passageways, selective means to supply concurrently hydrocarbons to the passageways in one of said chambers and a regenerating gas to the passageways in the other, selective means for concurrently passing a purging material through the catalytic material in one chamber to remove the iiuid hydrocarbons and in the other to remove the regeneration products,

and means for passing a temperature control medium through said closed conduits in each chamber.

a series of spaced closed conduits of substantial v` length in the direction of reactant ilow, said conduits having iins thereon arranged so that the ns on adjacent tubes dene passageways therebetween, catalyst material in said passageways, means for supplying reactant to said catalyst material, means for circulating a temperature control medium through said closed conduits, and means for heating said temperature control medium, the volume of catalyst constituting to 80 per cent of the space in the chamber.

5. An apparatus for the catalytic conversion of hydrocarbon oils comprising a reaction chamber, a series of spaced closed conduits of substantial length in the direction of reactant iiow, said conduits having iins thereon arranged so that the ns on adjacent tubes dene passageways therebetween, catalyst material in said passageways, means for supplying reactant to said catalyst material, means for circulating a temperature control medium through said closed conduits, and means for heating said temperature control medium, the volume of catalyst constituting 60 to 80 per cent of the space in the chamber, the volume of temperature control medium circulating in the chamber constituting 2 to 15 per cent oi the space in the chamber.

6. An apparatus for the catalytic conversion of hydrocarbon oils comprising a reaction chamber, a series of spaced closed metal conduits of substantial length in the direction of reactant v flow, said' conduits having ns thereon arranged so that the ns on adjacent tubes define passageways therebetween, catalyst material in said passageways, means for supplying reactant to said catalyst material, means for circulating a temperature control medium through said closed THOMAS P. SIMPSON. JOHN W. PAYNE.

JOHN A. CROWLEY, JR. CLARK S. TEITSWORTH. 

